Extraction process using supercritical carbon dioxide

ABSTRACT

The present invention provides a method of using CO 2  in an extraction process without the use of mechanical pumps to control CO 2  density. In particular, the invention relates to a process for extraction of one or more components from a plant material by manipulation of density of CO 2  in the extraction vessel via creating a temperature differential between the liquid CO 2  supply and the extraction vessel.

FIELD OF THE INVENTION

The present invention pertains to the field of the extraction of components from plant materials, more particularly, for extraction using supercritical carbon dioxide.

BACKGROUND OF THE INVENTION

Supercritical Fluid Extraction (SFE) is the process of separating one component (the extractant) from another (the matrix) using supercritical fluids as the extracting solvent. Extraction is usually from a solid matrix, but can also be from liquids. SFE can be used as a sample preparation step for analytical purposes, or on a larger scale to either strip unwanted material from a product (e.g. decaffeination) or collect a desired product (e.g. essential oils). Carbon dioxide (CO₂) is the most used supercritical fluid, sometimes modified by co-solvents such as ethanol or methanol. Extraction conditions for supercritical carbon dioxide occur above the critical temperature of 31° C. and critical pressure of 74 bar.

CO₂ can act as an effective solvent in both liquid and supercritical phases. CO₂ is known as a “tunable solvent” making it versatile for extracting a multitude of end products by controlling temperature, density and phase. These phase changes create an environment to extract differing weights of components from the plant material.

In the CO₂ system the solvating power can primarily be regarded as being a function of density and temperature within a static volume, with the solvent density being the more important factor. Heat provides kinetic energy thereby generally increasing solubility of target solutes, while varying CO₂ density provides ability to create a dissolution bias based on the solute's molecular attributes, such as symmetry, size and polarity in relation to the number of super critical carbon dioxide (SCCO₂) molecules required to dissolve individual solute molecules.

Currently known extraction methods using SCCO₂, involve density manipulation independent of temperature via specialized mechanical pumps to achieve extraction bias towards specific compounds. Typically, mechanical pumps are used to force liquid CO₂ at high pressure into a static volume to increase CO₂ density to the desired level, whereafter the temperature is manipulated to generate the desired SCCO₂ condition. As the SCCO₂ flows through the plant material, a variety of components (“solute”) can be dissolved in the SCCO₂. The extract-laden SCCO₂ is then transferred to another vessel where it is depressurized with the subsequent fall in density changing the SCCO₂ to gaseous CO₂, causing the solute to separate from the gaseous CO₂. The gaseous CO₂ is then subjected to a heat exchanger where it is cooled to liquid state and then pumped again to repeat the cycle.

For certain plant extracts (such as CBD cannabinoid solubility in CO₂ occurs when the density of CO₂ is 756 kg/m³—at around 53° C. at ˜2814 psi. At this density, the CO₂ is in supercritical phase and there are sufficient intermolecular spaces, and the spaces are of sufficient volume to hold CBD molecules in solution. If the density is higher, the spaces may become too small to accommodate the CBD molecules and if the density is too low, the spaces may be too large to hold the CBD in solution. In either case extraction efficiency is not optimal.

Liquid CO₂ is generally commercially available in supply tanks, often at ˜800 psi at ˜21° C., wherein ˜67% of CO₂ exists in liquid phase and ˜33% in gas phase. In this state the CO₂ tank is considered full, and combined density may be ˜550 kg/m³. If such a supply tank is connected to a constant volume extraction vessel, the pressures would equalize with the extraction vessel containing liquid and gas with a combined density of ˜550 kg/m³. This level of density may be insufficient for efficient encapsulation of the desired solute molecules and attempted extractions using this density will result in little or no extract. Therefore, mechanical pumps are used to physically force CO₂ into the extraction vessel until the desired density is reached.

U.S. Pat. No. 8,895,078, discloses a method for producing an extract from cannabis plant matter, containing tetrahydrocannabinol, cannabidiol and optionally the carboxylic acids thereof, wherein specific temperature/pressure combinations are presented for the various cannabinoids along with the use of mechanical pumps. In the method of this patent, pure CO₂ is conveyed via a conduit to a liquefier equipped with a condenser coil, and then liquid CO₂ is supplied via a pressurizing pump to a heat exchanger, to be available for the extraction cycle described therein.

In the Sandia National Laboratories 2010 report “Operation and Analysis of a Supercritical Braydon Cycle” (http://prod.sandia.gov/techlib/access-control.cgi/2010/100171.pdf), the descriptions and associated drawings clearly show mechanical pumps being used to control the density.

In extraction processes involving mechanical pumps, as the SCCO₂ is forced through the raw material at high rates, the SCCO₂ does not become fully impregnated, much less saturated with solute, and is subject to “channeling” whereby the SCCO₂ flow finds the path of least resistance, thereby bypassing some of the potential extracts. Different manufacturers have different flow rates and different ways of dealing with efficiency but they all function substantially in the same manner. Moreover, recycling of recovered CO₂ in these extraction processes can carry solute over into the pump causing the pump to malfunction and require service. Furthermore, mechanical pumps are expensive, noisy, and require high maintenance and often special infrastructure.

Hydrocarbon co-solvents have also been used in extraction processes involving SCCO₂. The hydrocarbon-enhanced extraction processes, however can leave residues in the extracts.

Accordingly, there is need for alternative cost effective and environmentally friendly extraction methods.

This background information is provided for the purpose of making known information believed by the applicant to be of possible relevance to the present invention. No admission is necessarily intended, nor should be construed, that any of the preceding information constitutes prior art against the present invention.

SUMMARY OF THE INVENTION

An object of the present invention is to provide a method of using CO₂ in an extraction process without the use of mechanical pumps to control CO₂ density. In accordance with an aspect of the present invention, there is provided a process of extracting one or more components from a plant material, the process comprising: a) providing a liquid-phase CO₂ supply at a known temperature; b) providing a predetermined amount of the plant material in a pressure regulated extraction vessel having known/constant volume; c) creating a temperature differential between the liquid-phase CO₂ supply and the extraction vessel, wherein the extraction vessel temperature is lower than the temperature of the liquid-phase CO₂ supply; d) allowing the liquid-phase CO₂ to flow into the extraction vessel due to the temperature differential, while maintaining the temperature differential between the liquid-phase CO₂ supply and the extraction vessel to load a target amount of the liquid-phase CO₂ to achieve a desired density of CO₂ in the extraction vessel; e) heating the extraction vessel to achieve supercritical-phase CO₂ at desired predetermined pressure and temperature; f) allowing the supercritical-phase CO₂ to reside in the extraction vessel at the predetermined temperature and pressure achieved in step e) for a time sufficient to ensure impregnation of the one or more components in the supercritical-phase CO₂; g) cooling the component-impregnated supercritical-phase CO₂ so that the component impregnated supercritical-phase CO₂ in the extraction vessel changes to component-impregnated liquid-phase CO₂; h) transferring the component-impregnated liquid-phase CO₂ into a collection vessel and decreasing the density of the liquid-phase CO₂ to convert the liquid-phase CO₂ into gaseous-phase CO₂, thereby allowing the one or more components to be separated from the CO₂; i) optionally collecting and cooling the gaseous-phase CO₂ in a pre-cooled recapture tank and recycling same for the extraction process.

BRIEF DESCRIPTION OF THE FIGURES

Further features and advantages of the present invention will become apparent from the following detailed description, taken in combination with the appended drawings, in which:

FIG. 1 illustrates a schematic representation of a CO₂ extraction plant involving the process in accordance to an embodiment of the present invention.

FIG. 2 illustrates a schematic representation of a CO₂ extraction plant involving the process in accordance to another embodiment of the present invention.

DETAILED DESCRIPTION OF THE INVENTION

Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.

The present invention provides a simplified, cost effective process for controlling phase and density of extraction solvent during extraction of desired components from a plant material, while using supercritical fluid (such as SCCO₂), wherein temperature/pressure/density relationship is controlled for maximal extraction selectivity without the use of mechanical pumps.

The inventor of the present invention has surprisingly established that the extraction of surface resident components from plant materials using carbon dioxide can be effectively achieved in the absence of mechanical pumps, by manipulation of density of CO₂ in the extraction vessel via creating a temperature differential between the liquid CO₂ supply and the extraction vessel. The process of the present invention requires less upfront cost, and lower ongoing production and maintenance costs.

The present invention provides a method of controlling phase change and density of CO₂ for extraction of desired extracts from a plant material using a combination of liquid CO₂ and supercritical CO₂ (SCCO₂). The method comprises providing a liquid-phase CO₂ supply at a known temperature and providing a predetermined amount of the plant material in a pressure regulated extraction vessel having known/constant volume. A temperature differential is created between the liquid-phase CO₂ supply and the extraction vessel, such that the extraction vessel temperature is lower than the temperature of the liquid-phase CO₂ supply. After achieving the desired temperature differential, the liquid-phase CO₂ is allowed to flow into the extraction vessel due to the temperature differential, while maintaining the temperature differential between the liquid-phase CO₂ supply and the extraction vessel, to load a desired/target amount of the liquid-phase CO₂ to achieve a desired density of CO₂ in the extraction vessel. The extraction vessel is then heated to achieve supercritical-phase CO₂ at desired predetermined pressure and temperature, sufficient for dissolving one or more extracts from the plant material.

In another aspect, the present invention provides a process of extracting components from a plant material. The process comprises providing a liquid-phase CO₂ supply at a known temperature and providing a predetermined amount of the plant material in a pressure regulated extraction vessel having known/constant volume. A temperature differential is created between the liquid-phase CO₂ supply and the extraction vessel, such that the extraction vessel temperature is lower than the temperature of the liquid-phase CO₂ supply. After achieving the desired temperature differential, the liquid-phase CO₂ is allowed to flow into the extraction vessel due to the temperature differential, while maintaining the temperature differential between the liquid-phase CO₂ supply and the extraction vessel, and loading a desired/target amount of the liquid-phase CO₂ to achieve a desired density of CO₂ in the extraction vessel. The extraction vessel is then heated to achieve supercritical-phase CO₂ at desired predetermined pressure and temperature sufficient for dissolving one or more extracts from the plant material. The supercritical-phase CO₂ is allowed to reside in the extraction vessel at the desired predetermined temperature and pressure for a time sufficient to ensure impregnation of the one or more components in the supercritical-phase CO₂. The component-impregnated supercritical-phase CO₂ is then cooled so that it changes to liquid-phase CO₂. The liquid-phase CO₂ impregnated with one or more components is then transferred into a collection vessel at a lower pressure or into a collection vessel with higher available volume, where density of the liquid-phase CO₂ is decreased to convert the liquid-phase CO₂ into gaseous-phase CO₂, thereby allowing the extracted components to be separated from the CO₂. The process optionally comprises collecting and cooling of the gaseous-phase CO₂ for conversion into liquid-phase CO₂ and recycling same in the extraction process.

The method and process of the present invention are suitable for extraction of one or more components from any plant material, particularly, surface resident components. In some embodiments, the method and process of the present invention are suitable for extraction of one or more cannabinoid components from cannabis plant material.

The temperature differential between the liquid-phase CO₂ supply and the extraction vessel can be created by heating the liquid-phase CO₂ supply and/or cooling the extraction vessel prior to and/or during CO₂ loading.

In some embodiments, the warmer liquid-phase CO₂ supply is optionally cooled prior to loading same into the extraction vessel.

In some embodiments, the liquid-phase CO₂ supply is obtained at a temperature higher than the initial temperature of the extraction vessel, thereby creating the desired temperature differential, and optionally cooling the extraction vessel before and/or during the loading of the liquid-phase CO₂ into the extraction vessel.

In some embodiments, the liquid-phase CO₂ supply is obtained at a temperature similar to the initial temperature of the extraction vessel, and the temperature differential is created by heating the liquid-phase CO₂ supply to a predetermined temperature above the temperature of the extraction vessel, and/or cooling the extraction vessel before and/or during the loading of the liquid-phase CO₂ into the extraction vessel.

In some embodiments, the liquid-phase CO₂ supply is obtained at a temperature lower than the initial temperature of the extraction vessel, and the temperature differential is created by first heating the liquid-phase CO₂ supply to a predetermined temperature above the temperature of the extraction vessel, optionally followed by cooling the extraction vessel before and/or during loading of the liquid-phase CO₂ into the extraction vessel.

Cooling of the extraction vessel can be achieved by the methods known in the art. In some embodiments, the extraction vessel is immersed in a heat transfer fluid (coolant) in a fluid bath. In some embodiments, the heat transfer fluid is circulated in a cooling jacket provided around the extraction vessel.

The heat transfer fluid is selected depending upon the desired temperature differential between the CO₂ supply and the extraction vessel. Non limiting examples of suitable heat transfer fluid include water, ethylene glycol, diethylene glycol, propylene glycol, Freon, mineral oils, silicone oils, etc. alone or in combination. In some embodiments, the heat transfer fluid is propylene glycol or a mixture of propylene glycol and water. In some embodiments, the heat transfer fluid is cold/hot water.

In some embodiments, the desired density of the liquid-phase CO₂ in the extraction vessel is from about 700 kg/m³ to about 850 kg/m³, which is achieved by loading a predetermined amount of liquid-phase CO₂.

In some embodiments, the predetermined amount of liquid-phase CO₂ to be loaded into the extraction vessel is from about 66% and 100% of the volume available in the extraction vessel.

The amount of liquid-phase CO₂ to be loaded into the extraction vessel can be calculated based on the value of the internal volume of the extraction vessel, excluding the plant material mass, and the desired density by using methods known in the art. For example, a correlation chart of CO₂ temperature, pressure and density (as shown in Tables 1a & 1b), can be first created using the density calculator such as the one published by Peace Software of Germany at http://www.peacesoftware.de/einigewerte/co2_e.html, as shown in the Table 2 below.

TABLE 1a CO2 - Temp/Pressure/Density Chart (kg/m3) Temp- Temp- Pressure Pressure Pressure Pressure Pressure Pressure Pressure Pressure Pressure Pressure Pressure Pressure C. F. 1000 1100 1200 1300 1400 1500 1600 1700 1800 1900 2000 2100 24 75 733 757 784 803 816 826 834 843 851 859 867 875 26 79 696 726 761 783 798 810 819 828 836 845 854 863 28 82 659 694 737 763 780 793 803 813 822 832 841 851 30 86 256 657 713 743 762 777 787 797 808 818 828 839 31 88 493 675 716 744 763 774 786 797 809 820 832 32 90 638 690 725 749 762 774 787 799 812 824 34 93 562 637 689 722 736 751 765 780 795 809 36 97 486 584 652 694 711 728 744 761 778 794 38 100 531 616 667 685 704 723 742 761 779 40 104 478 579 639 660 681 702 723 744 765 42 108 533 592 618 643 669 694 720 745 44 111 487 545 576 606 636 666 696 725 46 115 499 534 568 603 637 672 706 48 118 492 531 570 609 647 686 50 122 493 536 580 623 667 52 126 517 561 604 646 54 129 498 541 585 629 56 133 523 566 610 58 136 503 547 590 60 140 485 528 571 62 144 513 555 64 147 498 536 66 151 521 68 154 505 70 158 488

TABLE 1b CO2 - Temp/Pressure/Density Chart (kg/m3) Temp- Temp- Pressure Pressure Pressure Pressure Pressure Pressure Pressure Pressure Pressure Pressure Pressure Pressure C. F. 2200 2300 2400 2500 2600 2700 2800 2900 3000 3100 3200 3300 24 75 882 888 893 898 903 908 913 919 922 926 930 934 26 79 871 877 882 887 893 898 904 909 913 917 921 925 28 82 860 866 871 877 883 888 894 900 904 908 913 917 30 86 848 854 860 867 873 879 885 891 895 899 904 908 31 88 842 848 854 861 867 873 879 885 890 895 899 904 32 90 835 842 848 855 861 868 874 880 885 890 894 899 34 93 822 829 836 843 850 856 863 870 875 880 885 890 36 97 809 816 823 831 838 845 853 860 865 870 875 880 38 100 796 803 811 819 827 834 842 850 855 861 866 871 40 104 782 791 799 807 815 823 832 840 845 851 856 862 42 108 766 775 784 793 802 811 820 829 835 840 846 852 44 111 750 700 770 779 789 798 808 818 824 830 836 842 46 115 734 745 755 765 776 786 796 807 813 819 826 832 48 118 719 730 741 752 762 773 784 795 802 809 815 822 50 122 703 714 726 738 749 761 773 784 791 798 805 812 52 126 684 696 709 722 734 747 760 772 779 787 794 801 54 129 665 678 692 706 719 733 746 760 768 775 783 791 56 133 646 660 675 690 704 719 733 748 756 764 772 780 58 136 627 642 658 674 689 705 720 736 744 753 761 769 60 140 608 624 641 658 674 691 707 724 732 741 750 758 62 144 590 608 625 642 659 676 694 711 720 729 738 747 64 147 573 591 609 626 644 662 680 698 707 717 726 736 66 151 555 574 592 611 629 648 666 685 695 705 715 724 68 154 538 557 576 595 614 633 653 672 682 692 703 713 70 158 520 540 560 580 599 619 639 659 670 680 691 702

TABLE 2 Calculation of Thermodynamic State Variables of Carbon Dioxide Lower limit upper limit: 900 C, 1000 bar for calculation: −55 C, 1 bar Pressure: 2000 psi (lb/inch2) Temperature:  40 Celsius Calculate Property Value Unit Medium : carbon dioxide state of aggregation: overcritical fluid Pressure: 137.9 [ bar ] Temperature: 40 [ Celsius ] Density: 743.6128 [ kg/m³ ] Specific Enthalpy: 292.155 [ kJ/kg ] Specific Entropy: 1.27262 [ kJ/kg K ] Specific isobar 3.395096 [ kJ/kg K ] heat capacity: cp Specific isochor 0.9539754 [ kJ/kg K ] heat capacity: cv Isobar coefficient of 15.18083 [ 10⁻³ (1/K) ] thermal expansion: Heat conductance 83.66994 [ 10⁻³ (W/m * K) ] Dynamic viscosity: 62.9621 [ 10⁻⁶ (pa s) ] Kinematic viscosity: 0.084670543594731 [ 10⁻⁶ m²/s] Thermal diffusivity: 0.3659832 [ 10⁻⁷ m²/s] Prandtl-Number: 2.4712 Coefficient of 0.3114238 compressibility Z: speed of sound: 389.2818 [m/s] Once the correlation table is created, the weight of liquid CO₂ required to fill up to the desired capacity of an extraction vessel of known internal volume, can be calculated using conversion tables such as the one published by Universal Industrial Gases, Inc. of Easton, Pa. http://www.uigi.com/co2_conv.html, as shown in the Table 3 below.

TABLE 3 Unit Conversion Data for Carbon Dioxide Weight Gas Liquid Solid pounds tons kilograms cubic feet cu meters gallons liters cubic feet (lb) (t) (kg) (scf) (Nm³) (gal) (l) (cu ft) 1 pound 1.0 0.0005 0.4536 8.741 0.2294 0.11806 0.4469 0.010246 1 short ton 2000.0 1.0 907.2 17483 458.8 236.1 893.9 20.49 1 kilogram 2.205 0.0011023 1.0 19.253 0.5058 0.2603 0.9860 0.226 1 scf gas 0.1144 — 0.05189 1.0 0.02628 0.013508 0.05113 0.0011723 1 Nm³ gas 4.359 0.00218 1.9772 38.04 1.0 0.5146 1.948 0.04468 1 gal liquid 8.470 0.004235 3.842 74.04 1.9431 1.0 3.785 0.08678 1 liter 2.238 0.0011185 1.0151 19.562 0.5134 0.2642 1.0 0.02293 liquid 1 cu ft 97.56 0.0488 44.25 852.8 22.38 11.518 43.60 1.0 (solid) CO₂ liquid measured at 21.42 atmospheres and 1.7° F. CO₂ solid measured at 109.25° F. Scf (standard cubic foot) gas measured at 1 atmosphere and 70° F. Nm³ (normal cubic meter) gas measured at 1 atmosphere and 0° C. Liquid measured at 1 atmosphere and boiling temperature.

The amount of CO₂ loaded in to the extraction vessel can be measured directly via a weighing scale provided in association with the extraction vessel, or indirectly by measuring weight loss in liquid CO₂ supply tank.

Once the desired density of the liquid-phase CO₂ in the extraction vessel is achieved, the extraction vessel is heated to achieve supercritical-phase CO₂ at desired predetermined pressure and temperature. In some embodiments, the extraction vessel is heated by circulating a heat transfer fluid, which is heated to a temperature higher than the temperature of the extraction vessel. In some embodiments the extraction vessel is immersed in a fluid bath containing a heat transfer fluid, heated to a temperature higher than the temperature of the extraction vessel.

In some embodiments, the desired pressure is between 750 psi and 5,000 psi, and the desired temperature is between 24° C. and 75° C. The supercritical-phase CO₂ is allowed to reside in the extraction vessel for a time sufficient to ensure impregnation of one or more components from the plant material in the supercritical-phase CO₂. After achieving impregnation of supercritical-phase CO₂ with one or more components extracted from the plant material, the extraction vessel is cooled and the impregnated supercritical-phase CO₂ in the extraction vessel is converted to the impregnated liquid-phase CO₂.

The impregnated liquid-phase CO₂ is transferred into a collection vessel, wherein density of the liquid-phase CO₂ is decreased to convert the liquid-phase CO₂ into gaseous-phase CO₂, thereby allowing the impregnated components to be separated. In some embodiments, the liquid-phase CO₂ impregnated with one or more components is flushed into a collection vessel. The flushing effect of the liquid CO₂ enhances the movement of the solute from the extraction vessel to the collection vessel thus increasing the efficiency of the extraction. This is particularly effective when the desired components are surface-resident on the plant material.

In some embodiments, the gaseous-phase CO₂ that is exhausted from the collection vessel is collected and cooled in a recapture tank for re-use in the extraction process. In some embodiments, the gaseous-phase CO₂ is collected in pre-cooled recapture tank.

The present invention provides a temperature differential “pump” wherein the temperature differential between the CO₂ supply and the extraction vessel is utilized to achieve desired density of CO₂ in the extraction vessel, rather than the use of mechanical pumps to continuously “brute force” the density, and bulk flow rate to move the extracts to the collector. An additional economic benefit of being able to quickly heat and cool the extraction vessel is that multiple cycles can be run during an operating day.

It is believed that the temperature differential slows down the relative molecular movement of the CO₂ between the liquid CO₂ supply and the extraction vessel during loading, which makes the CO₂ more dense and allows more molecules to move into the same space at the lower temperature, thereby increasing density within a volume that would normally not be fillable with the higher density without the temperature differential.

In some embodiments, the process of the present invent comprises: a) providing a liquid-phase CO₂ supply at a known temperature; b) providing a predetermined amount of the plant material in a pressure regulated extraction vessel having known/constant volume; c) heating the a liquid-phase CO₂ supply, and cooling the extraction vessel thereby creating a temperature differential between the liquid-phase CO₂ supply and the extraction vessel, wherein the extraction vessel temperature is lower than the temperature of the liquid-phase CO₂ supply; d) allowing CO₂ from the liquid-phase CO₂ to flow into the extraction vessel due to the temperature differential, while maintaining the temperature differential between the liquid-phase CO₂ supply and the extraction vessel to load a target amount of the CO₂ to achieve a desired density of CO₂ in the extraction vessel; e) heating the extraction vessel to achieve supercritical-phase CO₂ at desired predetermined pressure and temperature; f) allowing the supercritical-phase CO₂ to reside in the extraction vessel at the predetermined temperature and pressure achieved in step e) for a time sufficient to ensure impregnation of the one or more components in the supercritical-phase CO₂; g) cooling the component-impregnated supercritical-phase CO₂ so that the component impregnated supercritical-phase CO₂ in the extraction vessel changes to component-impregnated liquid-phase CO₂; h) transferring the component-impregnated liquid-phase CO₂ into a collection vessel and decreasing the density of the liquid-phase CO₂ to convert the liquid-phase CO₂ into gaseous-phase CO₂, thereby allowing the one or more components to be separated from the CO₂; i) optionally collecting and cooling the gaseous-phase CO₂ in a pre-cooled recapture tank and recycling same for the extraction process.

The process of the present invention can be applied to extraction methods involving other super critical fluids.

To gain a better understanding of the invention described herein, the following examples are set forth. It will be understood that these examples are intended to describe illustrative embodiments of the invention and are not intended to limit the scope of the invention in any way.

FIGS. 1 and 2 illustrate schematic representations of CO₂ extraction plants for conducting the process in accordance with exemplary embodiments of the present invention.

Example: 1

Referring to FIG. 1, a liquid CO₂ supply is obtained as a pressurized tank 2, which is connected fluidically to a pressure regulated extraction vessel 10 via loading Line 6 provided with a shutoff valve 8. Optionally liquid CO₂ supply tank 2 is placed in a warm fluid bath 4 to heat the liquid CO₂ in the pressurized tank 2 to a predetermined temperature.

In this example, the extraction vessel 10 is positioned in a fluid bath 14 which during CO₂ loading is filled with cold heat exchange fluid to remove heat thereby causing a decrease in the temperature of the extraction vessel, and creating a temperature differential between the warmer liquid CO₂ supply and the extraction vessel. The extraction vessel 10 is further fluidically connected to a collection vessel 24 via connector line 20 provided with a release valve 22. A recapture/exhaust line 26 connects the collection vessel 24 and the CO₂ recapture tank 28, which in this example is positioned in a cold fluid bath 30. The amount of liquid CO₂ being loaded into the extraction vessel is measured via a weighing scale 16.

In this example, the process is carried out by placing a predetermined amount of a plant material 18 in the pressure regulated extraction vessel 10, which is then sealed. Shutoff valve 8 is opened causing liquid CO₂ to flow from the liquid CO₂ supply tank 2 to the cooling extraction vessel 10. As the heat differential causes the liquid CO₂ to flow from the liquid CO₂ supply tank 2 to the extraction vessel 10, the weight of the liquid CO₂ in the extraction vessel rises and is monitored by the weigh scale 16 or weigh scale 31—the higher the weight in extraction vessel 10, the higher the CO₂ density level in the extraction vessel 10.

Once the desired amount of CO₂ is loaded into the extraction vessel 10 to achieve the desired density, the heat exchange fluid in fluid bath 14 is changed from cold to hot fluid, to heat the liquid-phase CO₂ in the extraction vessel at a predetermined pressure as indicated by the pressure gauge 12 to achieve supercritical-phase CO₂. The fluid temperature in the extraction vessel 10 and fluid bath 14 can be increased or decreased, and maintained as required by adding hotter or colder fluid.

Once the extraction vessel has reached the desired pressure, the supercritical-phase CO₂—and plant material 18 are allowed to reside in the extraction vessel for a desired length of time. Once the desired length of time has lapsed, the warm fluid in the extraction vessel fluid bath 14 is changed to cold fluid causing a cooling of the extractor vessel and a phase change from supercritical-phase CO₂ to liquid-phase CO₂ at a predetermined pressure as displayed by the pressure gauge 12. Once the phase change is complete, liquid-phase CO₂ impregnated with one or more extracted solute components is transferred from the extraction vessel to collection vessel 24 via collection line 20 regulated by relief valve 22. As the liquid CO₂ enters the collection vessel 24, the additional volume allows rapid reduction of the CO₂ density causing the liquid-phase CO₂ to change to gaseous phase CO₂ resulting in separation/precipitation of the impregnated/extracted components 29 from CO₂.

In some embodiments, the velocity of the evacuating liquid CO₂ also provides a flushing effect that carries extract from the plant material to the collection vessel 24, increasing the overall efficiency of the extraction process.

Gaseous CO₂ is then transferred to pre-cooled recapture tank 28 placed in a cooled fluid bath 30.

Once the weight of CO₂ in the extraction vessel declines to a predetermined weight, the extraction cycle is complete and the remaining gaseous CO₂ in the extraction vessel is “topped-up” for another extraction cycle on the same raw plant material, with the same or other CO₂ density/pressure, or the remaining CO₂ in the extraction vessel is vented and the extracted raw plant material is replaced for additional extraction cycles.

Example: 2

Referring to FIG. 2, a liquid CO₂ supply obtained as a pressurized tank 32 is fluidically connected to an extraction vessel 40 through loading line 36, provided with a shutoff valve 38. In this embodiment, the extraction vessel 40 is surrounded by a jacket 44 through which cooling fluid 52 from freezer 50 is circulated via connector line 54 provided with a valve 56 to remove heat and thereby causing a decrease in extraction vessel temperature and a temperature differential between the CO₂ supply and the extraction vessel. Optionally, heater 34 is provided to heat the liquid CO₂ in the pressurized tank 32 to a predetermined temperature.

The extraction vessel 40 is also fluidically connected to a heat reservoir 62 via a connector line 58 provided with a valve 60. The extraction vessel is further fluidically connected to a collection vessel 70 via connector line 66 provided with a release valve 68. A recapture line 74 connects the collection vessel 70 and the recapture tank 76, which in this example is placed in freezer 78 containing coolant 80.

Valves 56 and 60 are provided to facilitate switching of the circulating fluid from cold fluid to hot fluid to maintain the extraction vessel temperature in a predetermined range. Valves 38, 56, 60 and 68 are operated manually or electromechanically. In an alternative example, the valves are programmed for automatic operation.

The coolant jacket 44 is sealed or open to the atmosphere and the circulation of the cool and/or hot heat transfer fluid is caused by available pressurized hot/cold heat transfer fluid supply. In an alternative example, the circulation of the cool and/or hot heat transfer fluid is further supplemented with local pumps, such as 82 and 84.

In this example, the process is carried out by placing a predetermined amount of a plant material 48 in the pressure regulated extraction vessel 40, which is then sealed. Shutoff valve 56 is opened and coolant 52 is circulated through the coolant jacket 44 causing a transfer of heat from the extraction vessel to freezer 50.

Valve 38 is then opened causing liquid CO₂ to flow from the liquid CO₂ supply 32 to the cooling extraction vessel 40. As the liquid CO₂ flows through the loading line 36, it adds heat to the extraction vessel 40, which is removed by the circulating coolant 52 and transferred to freezer 50. As the heat differential causes the CO₂ to flow from the CO₂ supply 32 to the extraction vessel 40, the weight of the CO₂ in the extraction vessel rises and is monitored by the weigh scale 46—the higher the weight, the higher the CO₂ density level in the extraction vessel. Once the loaded CO₂ reaches a predetermined amount to achieve a desired density, shutoff valve 56 and shutoff valve 38 are closed, and shutoff valve 60 is opened causing circulation of the hot heat transfer fluid 64 through the coolant jacket 44. The plant material and CO₂ in the extraction vessel are heated by the circulating hot fluid up to a predetermined pressure as indicated by the pressure gauge 42 to achieve supercritical-phase CO₂.

Once the desired pressure is reached, shut off valve 60 is closed, and the supercritical-phase CO₂ and plant material 48 allowed to reside in the extraction vessel for a predetermined time. If the extraction vessel pressure falls below the desired value, valve 60 is re-opened to add heat.

Once the predetermined resident time has elapsed, shutoff valve 60 is closed, shutoff valve 56 is opened to circulate cooled fluid 52 through the coolant Jacket 44 to cool the extraction vessel to the point that the supercritical-phase CO₂ in the extraction vessel changes to liquid-phase CO₂ at a predetermined pressure as displayed by the pressure gauge 42.

Once the supercritical-phase CO₂ in the extraction vessel is converted to liquid-phase CO₂, shutoff valve 56 is closed. Shutoff valve 68 is then modulated to release liquid-phase CO₂ impregnated with one or more solute components to collection vessel 70, where the liquid-phase CO₂ changes to gaseous-phase CO₂, and the impregnated components 85 get separated from CO₂. Gaseous CO₂ is then transferred to pre-cooled recapture tank 76 placed in coolant 80 in freezer 78.

Optionally, band heat 72 provides heat to the gaseous-phase CO₂, accelerating the flow of solute-free gaseous CO₂ along the recapture line 74, and into the pre-cooled recapture tank 76 placed in coolant 80 in freezer 78.

Once the weight of CO₂ in the extraction vessel declines to a predetermined weight, the extraction cycle is complete and the remaining CO₂ in the extraction vessel is “topped-up” for another extraction cycle on the same raw plant material, with the same or other CO₂ density/pressure, or the remaining CO₂ in the extraction vessel is vented and the extracted raw plant material is changed for additional extraction cycles.

As evident from the above discussion, the present invention provides a cost effective, simplified extraction process, which eliminates the number of mechanical pumps in the density control process.

Although the invention has been described with reference to certain specific embodiments, various modifications thereof will be apparent to those skilled in the art without departing from the spirit and scope of the invention. All such modifications as would be apparent to one skilled in the art are intended to be included within the scope of the following claims. 

The embodiments of the invention in which an exclusive property or privilege is claimed are defined as follows:
 1. A process of extracting one or more components from a plant material, the process comprising: a) providing a liquid-phase CO₂ supply at a known temperature; b) providing a predetermined amount of the plant material in a pressure regulated extraction vessel having known/constant volume; c) creating a temperature differential between said liquid-phase CO₂ supply and the extraction vessel, wherein the extraction vessel temperature is lower than the temperature of the liquid-phase CO₂ supply; d) allowing CO₂ from liquid-phase CO₂ supply to flow into the extraction vessel due to the temperature differential, while maintaining the temperature differential between the liquid-phase CO₂ supply and the extraction vessel to load a target amount of the CO₂ to achieve a desired density of CO₂ in the extraction vessel; e) heating said extraction vessel to achieve supercritical-phase CO₂ at desired predetermined pressure and temperature; f) allowing said supercritical-phase CO₂ to reside in said extraction vessel at said predetermined temperature and pressure achieved in step e) for a time sufficient to ensure impregnation of the one or more components in the supercritical-phase CO₂; g) cooling said component-impregnated supercritical-phase CO₂ so that the component-impregnated supercritical-phase CO₂ in the extraction vessel changes to component-impregnated liquid-phase CO₂; and h) transferring said component-impregnated liquid-phase CO₂ into a collection vessel at a pressure lower than that of the extraction vessel and/or into a collection vessel with higher available volume, thereby decreasing the density of said liquid-phase CO₂ to convert said liquid-phase CO₂ into gaseous-phase CO₂, thereby allowing the one or more components to be separated from the CO₂.
 2. The process of claim 1, wherein said liquid-phase CO₂ supply is obtained at a temperature same or similar as the temperature of the extraction vessel, and the temperature differential is created by heating the liquid-phase CO₂ supply to a predetermined temperature above the temperature of the extraction vessel and/or cooling the extraction vessel before and/or during the loading of the liquid-phase CO₂ into the extraction vessel.
 3. The process of claim 1, wherein said liquid-phase CO₂ supply is obtained at a temperature lower that the temperature of the extraction vessel, and the temperature differential is created by first heating said liquid-phase CO₂ supply to a predetermined temperature above the temperature of the extraction vessel, optionally followed by cooling the extraction vessel before and/or during loading of the liquid-phase CO₂ into the extraction vessel.
 4. The process of claim 1, wherein said liquid-phase CO₂ supply is obtained at a temperature higher than the initial temperature of the extraction vessel, thereby creating the desired temperature differential, and optionally cooling the extraction vessel before and/or during the loading of the liquid-phase CO₂ into the extraction vessel.
 5. The process of claim 1, wherein said extraction vessel is cooled via a heat transfer fluid.
 6. The process of claim 5, wherein said heat transfer fluid is one or more of air, water, ethylene glycol, diethylene glycol, propylene glycol, mineral oils, or silicone oils.
 7. The process of claim 1, wherein said desired density is about 700 kg/m³ to about 850 kg/m³.
 8. The process of claim 1, wherein said predetermined amount of liquid-phase CO₂ in step d) is between 66% and 100% of the volume available in the extraction vessel containing the plant material.
 9. The process of claim 1, wherein in step e) the predetermined pressure is between 750 psi and 5,000 psi and the temperature is between 24° C. and 75° C.
 10. The process of claim 1, further comprising collecting and cooling said gaseous-phase CO₂ in a pre-cooled recapture tank and recycling same for the extraction process. 